EP4249523A1 - Poudre de polyéthylène et corps moulé - Google Patents

Poudre de polyéthylène et corps moulé Download PDF

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Publication number
EP4249523A1
EP4249523A1 EP21894564.0A EP21894564A EP4249523A1 EP 4249523 A1 EP4249523 A1 EP 4249523A1 EP 21894564 A EP21894564 A EP 21894564A EP 4249523 A1 EP4249523 A1 EP 4249523A1
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EP
European Patent Office
Prior art keywords
polyethylene powder
kneading
polymerization
ethylene
less
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EP21894564.0A
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German (de)
English (en)
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EP4249523A4 (fr
Inventor
Naoya Okitsu
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Asahi Kasei Corp
Asahi Chemical Industry Co Ltd
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Asahi Kasei Corp
Asahi Chemical Industry Co Ltd
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Publication of EP4249523A1 publication Critical patent/EP4249523A1/fr
Publication of EP4249523A4 publication Critical patent/EP4249523A4/fr
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    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F10/02—Ethene
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J3/00—Processes of treating or compounding macromolecular substances
    • C08J3/12—Powdering or granulating
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F210/00—Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F210/16—Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J3/00—Processes of treating or compounding macromolecular substances
    • C08J3/005—Processes for mixing polymers
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J5/00—Manufacture of articles or shaped materials containing macromolecular substances
    • C08J5/18—Manufacture of films or sheets
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
    • C08L23/00—Compositions of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Compositions of derivatives of such polymers
    • C08L23/02—Compositions of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Compositions of derivatives of such polymers not modified by chemical after-treatment
    • C08L23/04—Homopolymers or copolymers of ethene
    • C08L23/08—Copolymers of ethene
    • C08L23/0807—Copolymers of ethene with unsaturated hydrocarbons only containing more than three carbon atoms
    • C08L23/0815—Copolymers of ethene with aliphatic 1-olefins
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M50/00—Constructional details or processes of manufacture of the non-active parts of electrochemical cells other than fuel cells, e.g. hybrid cells
    • H01M50/40—Separators; Membranes; Diaphragms; Spacing elements inside cells
    • H01M50/409—Separators, membranes or diaphragms characterised by the material
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M50/00—Constructional details or processes of manufacture of the non-active parts of electrochemical cells other than fuel cells, e.g. hybrid cells
    • H01M50/40—Separators; Membranes; Diaphragms; Spacing elements inside cells
    • H01M50/409—Separators, membranes or diaphragms characterised by the material
    • H01M50/411—Organic material
    • H01M50/414—Synthetic resins, e.g. thermoplastics or thermosetting resins
    • H01M50/417—Polyolefins
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F110/00—Homopolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F110/02—Ethene
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2323/00—Characterised by the use of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Derivatives of such polymers
    • C08J2323/02—Characterised by the use of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Derivatives of such polymers not modified by chemical after treatment
    • C08J2323/04—Homopolymers or copolymers of ethene
    • C08J2323/06—Polyethene
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2323/00—Characterised by the use of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Derivatives of such polymers
    • C08J2323/02—Characterised by the use of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Derivatives of such polymers not modified by chemical after treatment
    • C08J2323/04—Homopolymers or copolymers of ethene
    • C08J2323/08—Copolymers of ethene
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
    • C08L2207/00—Properties characterising the ingredient of the composition
    • C08L2207/06—Properties of polyethylene
    • C08L2207/068—Ultra high molecular weight polyethylene
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
    • C08L2314/00—Polymer mixtures characterised by way of preparation
    • C08L2314/02—Ziegler natta catalyst
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/10—Energy storage using batteries

Definitions

  • the present invention relates to a polyethylene powder and a molded article.
  • ultra-high-molecular-weight polyethylene powders are molded by various molding methods, such as melt drawing, injection molding, extrusion molding, and compression molding, and used for various applications, such as films, sheets, microporous membranes, fibers, foams, and pipes.
  • various molding methods such as melt drawing, injection molding, extrusion molding, and compression molding
  • applications such as films, sheets, microporous membranes, fibers, foams, and pipes.
  • microporous membranes are used for separators, which are important components of lithium-ion batteries and lead-acid batteries.
  • battery separators In addition to a function to allow only ions to pass through while separating the positive and negative electrodes, battery separators have a shutdown function to prevent the battery reaction from going out of control by blocking the passage of ions by melting the pores when a large current flows, in other words, a function to close the pores at a temperature lower than the temperature at which a thermal runaway occurs, a so-called fuse effect. There is a need to improve this shutdown function.
  • Battery separators are also required to have high mechanical strength.
  • a wet extrusion method is generally used to extrude polyethylene powders while dissolving them in solvents.
  • a wet extrusion method is generally used to extrude polyethylene powders while dissolving them in solvents.
  • the dispersibility of the polyethylene powders in solvents is poor, unmelted materials are generated, leading to filter clogging in the extruder and worsening the appearance of the separators. Therefore, improvement of the dispersibility of polyethylene powders in solvents has been required for the improvement of the appearance.
  • the long-term stability of battery separators means that the microporous membrane has a uniform pore structure, so that there is no bias in ion transmission, and short circuit and degradation over time are less likely to occur.
  • Patent Literature 1 discloses a polyethylene resin composition comprising an ethylene homopolymer having a specific melt flow rate, a specific molecular weight distribution, and a specific elution volume measured by cross-fractionation chromatography.
  • Patent Literature 2 discloses a battery separator comprising three polyethylenes with different physical properties, and having a low shutdown temperature and constant membrane strength and air permeability.
  • Patent Literature 3 discloses a battery separator having excellent long-term storage stability, high yield, and high output characteristics.
  • Patent Literature 4 discloses a technique of imparting predetermined particle size distribution and a predetermined swelling ratio at the same time.
  • Patent Literature 5 discloses a polyethylene resin composition produced by multistage polymerization and a molded article thereof, the polyethylene resin composition having excellent moldability, durability, and impact strength, wherein when the polyethylene resin composition is formed into a molded article, unevenness derived from high-molecular-weight gel is less likely to occur, and it is possible to produce a molded article with an excellent appearance.
  • Patent Literature 1 has excellent mechanical strength, air permeability, and processability, but a problem is that there is still room for improvement of shutdown function and long-term stability.
  • Patent Literature 2 no consideration has been made to improve the dispersibility of the resin in the extrusion solvent, and a problem is that components with the highest molecular weight remain in the microporous membrane as unmelted materials, possibly causing deterioration in appearance. At locations where high-molecular-weight components are unevenly distributed in the microporous membrane, partial shrinkage is likely to occur due to the strong entanglement of molecular chains, and the pore structure of the microporous membrane becomes non-uniform, which causes problems of uneven ion transmission and poor long-term stability.
  • Patent Literature 3 a problem is that no consideration has been made to improve the shutdown function of the battery separator.
  • Patent Literatures 4 and 5 a problem is that no consideration has been made to improve the long-term stability and shutdown function of the battery separator.
  • an object of the present invention is to provide a polyethylene powder that can give a microporous membrane having an excellent appearance, high shutdown function, and a uniform pore structure, and thus serving as a battery separator with excellent long-term stability.
  • a polyethylene powder that can achieve the above object can be obtained by identifying the slope of a straight line connecting two local maximum points in a torque curve obtained when kneading the polyethylene powder under predetermined kneading conditions.
  • the present invention has been completed.
  • the present invention is as described below.
  • the present invention can provide a polyethylene powder that can give a microporous membrane having an excellent appearance, high shutdown function, and a uniform pore structure, and thus serving as a battery separator with excellent long-term stability.
  • Figure 1 shows an example of the torque curve of the polyethylene powder.
  • the polyethylene powder of the present embodiment has a viscosity average molecular weight of 100,000 or more and 2,500,000 or less, and
  • the polyethylene powder of the present embodiment has the above configuration, a microporous membrane used as a battery separator having an excellent appearance, high shutdown function, and excellent long-term stability due to a uniform pore structure can be obtained.
  • the long-term stability of battery separators means that the microporous membrane has a uniform pore structure, so that there is no bias in ion transmission, and short circuit and degradation over time are less likely to occur.
  • the polyethylene powder of the present embodiment (hereinafter also referred to simply as "the powder") is composed of an ethylene-based polymer.
  • ethylene-based polymer examples include an ethylene homopolymer, and a copolymer of ethylene and other comonomers copolymerizable with ethylene (e.g., a binary or ternary copolymer).
  • the bonding form of the copolymer may be random or block.
  • Examples of other comonomers copolymerizable with ethylene include, but are not particularly limited to, ⁇ -olefins, vinyl compounds, and the like. Other comonomers can be used singly or in combination of two or more.
  • ⁇ -olefins include, but are not particularly limited to, C 3-20 ⁇ -olefins, and specific examples include propylene, 1-butene, 4-methyl-1-pentene, 1-hexene, 1-octene, 1-nonene, 1-decene, 1-undecene, 1-dodecene, 1-tridecene, and 1-tetradecene.
  • other comonomers are preferably propylene and/or 1-butene, in terms of further enhancing the heat resistance and strength of the microporous membrane.
  • vinyl compounds include, but are not particularly limited to, vinyl cyclohexane, styrene, and derivatives thereof.
  • non-conjugated polyenes such as 1,5-hexadiene and 1,7-octadiene, may also be used as other comonomers.
  • the polyethylene powder of the present embodiment has a viscosity average molecular weight (Mv) of 100,000 or more and 2,500,000 or less, preferably 200,000 or more and 2,000,000 or less, and more preferably 250,000 or more and 1,200,000 or less.
  • Mv viscosity average molecular weight
  • the viscosity average molecular weight (Mv) of the polyethylene powder can be controlled within the above numerical range by appropriately adjusting the polymerization conditions described later. Specifically, the viscosity average molecular weight (Mv) can be controlled, for example, by allowing hydrogen to be present as a chain transfer agent in the polymerization system or changing the polymerization temperature.
  • the microporous membrane containing the polyethylene powder of the present embodiment has sufficient mechanical strength.
  • the viscosity average molecular weight (Mv) is 2,500,000 or less
  • the polyethylene powder of the present embodiment has excellent molding processability, such as dispersibility in solvents and stretchability. Therefore, microporous membranes molded by using the polyethylene powder of the present embodiment have few unmelted materials and thickness deviation, and an excellent appearance.
  • indexes for estimating the impregnability of a plasticizer into the polyethylene powder include powder pore physical properties and solubility under static conditions.
  • One of the most important factors that determine the physical properties of microporous membranes molded by using the polyethylene powder is the entanglement state of molecular chains of polyethylene formed during extrusion.
  • the entanglement state of molecular chains can be accurately evaluated by using the indexes under predetermined extrusion conditions.
  • the slope of a straight line connecting two local maximum points in a torque curve obtained under predetermined kneading conditions is identified to thereby evaluate simultaneously and accurately the impregnability of the plasticizer into the polyethylene powder and the physical properties of the microporous membrane.
  • the slope of a straight line connecting two local maximum points in a torque curve obtained when kneading the polyethylene powder of the present embodiment using a Labo Plastomill Mixer, produced by Toyo Seiki Seisaku-sho, Ltd. (unit model: 30C150, mixer model: R-60) under the following ⁇ Kneading Conditions> is 2 N ⁇ m/min or more and 15 N ⁇ m/min or less, whereby a polyethylene powder that is very suitable as a raw material for microporous membranes can be obtained.
  • Fig. 1 shows an example of the torque curve.
  • Fig. 1 the average torque (rotational load generated during kneading) (N ⁇ m) when kneading the powder under predetermined kneading conditions is plotted on the vertical axis, and the kneading time (min) is plotted on the horizontal axis.
  • the solid line indicates the average torque
  • the dashed line indicates the set temperature.
  • the range of the slope of a straight line connecting two local maximum points in the torque curve obtained when kneading the polyethylene powder of the present embodiment under the above ⁇ kneading Conditions> is 2 N ⁇ m/min or more and 15 N ⁇ m/min or less, preferably 3 N ⁇ m/min or more and 12 N ⁇ m/min or less, and more preferably 5 N ⁇ m/min or more and 10 N ⁇ m/min or less.
  • the slope of a straight line connecting two local maximum points in the torque curve obtained when kneading the polyethylene powder under the above ⁇ Kneading Conditions> is 2 N ⁇ m/min or more, it is possible to suppress the generation of unmelted materials, and it tends to be possible to produce a microporous membrane with an excellent appearance. Further, because the slope is 2 N ⁇ m/min or more, an uneven entanglement state of molecular chains in the polyethylene powder can be homogenized; thus, a microporous membrane molded by using the polyethylene powder of the present embodiment tends to have a uniform pore structure and excellent long-term stability.
  • the slope is 15 N ⁇ m/min or less, the fluidity of polyethylene is good during melting, and it tends to be possible to produce a microporous membrane in which pores are likely to be clogged during shutdown.
  • a polyethylene powder has many pores, and when such a polyethylene powder is extruded in a plasticizer, the plasticizer impregnates through these pores. If the polyethylene powder has a pore structure that makes it difficult for the plasticizer to impregnate, before the plasticizer impregnates the center of the polyethylene powder, the temperature of the polyethylene powder reaches the melting point or higher and melting starts, thus clogging the pores. The center of the polyethylene powder that cannot come into contact with the plasticizer has poor dispersibility, and as a result, the powder tends to remain as unmelted materials. In particular, this tendency becomes even stronger when the molecular weight of the polyethylene powder is high.
  • the polyethylene powder of the present embodiment has a fast impregnation speed of plasticizers and good dispersibility; thus, it is possible to suppress unmelted materials.
  • the entanglement state of molecular chains formed when extruding the polyethylene powder in a plasticizer correlates with the entanglement state of molecular chains in the microporous membrane obtained by stretching after extrusion. Therefore, if the entanglement state of molecular chains formed during extrusion is not uniform, the microporous membrane will have areas with strong and weak entanglement of molecular chains. Areas with strong entanglement of molecular chains in the microporous membrane tend to shrink and the pores become smaller, while the pores in the surrounding areas are expanded. Since a larger amount of ions passes through areas with expanded pores, when the microporous membrane is used as a battery separator, degradation and short circuit tend to occur more easily during repeated charging and discharging. Further, if the entanglement of molecular chains is too strong, fluidity at the shutdown temperature tends to deteriorate.
  • the polyethylene powder of the present embodiment is extruded to form a uniform and moderate entanglement state of molecular chains; thus, microporous membranes obtained after extrusion have a uniform pore structure, and their pores are easily clogged during shutdown.
  • the polyethylene powder has a pore structure facilitating impregnation with a plasticizer, and that the entanglement state of molecular chains in the polyethylene powder can be easily homogenized in the kneading process.
  • the characteristics of the polyethylene powder that satisfies these requirements are, for example, that the pores on the surface of the polyethylene powder are expanded, and that there is less entanglement of molecular chains on the surface of the polyethylene powder.
  • comonomers are copolymerized in a flash tank located between reactors in the multistage polymerization process, and comonomers are introduced into a flash tank located after the reactor to post-polymerize a low-density ethylene copolymer.
  • a torque curve is obtained by plotting the average torque (rotational load generated during kneading) [N ⁇ m] calculated by Labo Plastomill Mixer Test Program Ver. 4.52 (Copyright (C) Toyo Seiki Seisaku-sho, Ltd.) on the vertical axis, and the kneading time [min] on the horizontal axis. At this time, the average torque value is plotted every 0.125 seconds. Then, the elapsed times and torque values when the maximum value is shown are read.
  • the polyethylene powder and the antioxidant are preferably mixed in advance in a resin container.
  • the liquid paraffin used in the above ⁇ Kneading Conditions> may be any liquid paraffin that acts as a plasticizer, and that can form, when kneaded with the polyethylene powder, a homogeneous solution at a temperature equal to or higher than the melting point of the polyethylene powder.
  • Liquid paraffin refers to the purest hydrocarbon compound (oil) refined to a high degree of purity by removing impurities, such as aromatic hydrocarbons and sulfur compounds, contained in petroleum lubricating oil fractions with sulfuric anhydride and fuming sulfuric acid. Liquid paraffin is colorless, transparent, tasteless, and odorless, and examples include white oil, mineral oil, and the like.
  • the antioxidant used in the above ⁇ Kneading Conditions> is preferably a phenol-based antioxidant, which is a primary antioxidant.
  • examples include, but are not particularly limited to, 2,6-di-t-butyl-4-methylphenol, pentaerythrityl tetrakis-[3-(3,5-di-t-butyl-4-hydroxyphenyl)propionate], octadecyl 3-(3,5-di-t-butyl-4-hydroxyphenyl)propionate, and the like.
  • the torque curve obtained when kneading the polyethylene powder under the above ⁇ Kneading Conditions> has a first peak obtained such that the polyethylene powder is impregnated with a plasticizer and swollen, and a second peak obtained such that the polyethylene powder is dissolved and dispersed in the plasticizer.
  • the time from the observation of a local maximum point A during the first peak to the observation of a local maximum point B during the second peak corresponds to the time required from impregnation of the polyethylene powder with the plasticizer to dispersion of the polyethylene powder in the plasticizer.
  • the difference in rotational load generated during kneading which is the value on the vertical axis between the first local maximum point A and the second local maximum point B, corresponds to the viscosity change of the system before and after dispersion of the polyethylene powder. The better the dispersibility of the polyethylene powder and the stronger the entanglement of molecular chains formed in the kneading process, the greater this change.
  • the slope of the straight line connecting the two local maximum points in the torque curve of the present embodiment can be more specifically measured by the method described in the Examples, described later.
  • the ratio of kneading energy (E A ) during swelling to kneading energy (E B ) during melting, (E A /E B ), is preferably 0.02 or more and 0.3 or less, more preferably 0.02 or more and 0.2 or less, and even more preferably 0.02 or more and 0.1 or less.
  • the kneading energy (E A ) during swelling in the torque curve obtained when kneading the polyethylene powder of the present embodiment under the above ⁇ Kneading Conditions> is an integrated value of torque per unit volume from the point where the temperature rise starts until the local minimum point between the first and second peaks is reached. This value increases as a larger amount of plasticizer is incorporated into the polyethylene powder.
  • the kneading energy (E B ) during melting in the present embodiment is an integrated value of torque per unit volume from the local minimum point between the first and second peaks to the end of kneading. This value increases as the entanglement of molecular chains formed in the kneading process is stronger.
  • the ratio of kneading energy (E A ) during swelling to kneading energy (E B ) during melting, (E A /E B ), is 0.02 or more, a moderate amount of plasticizer is incorporated into the polyethylene powder during swelling, and the generation of unmelted materials is further suppressed. Further, the fluidity of the polyethylene resin during melting tends to be improved. Therefore, it tends to be possible to produce a microporous membrane with a more excellent appearance and more enhanced shutdown function.
  • the ratio of kneading energy (E A ) during swelling to kneading energy (E B ) during melting, (E A /E B ), in the torque curve obtained when kneading the polyethylene powder of the present embodiment under the above ⁇ Kneading Conditions> can be specifically measured by the method described in the Examples.
  • the ratio (E A /E B ) can be controlled within the above numerical range by adjusting the molecular weight and density of polyethylene generated in the first half of the polymerization process, and adjusting the molecular weight and density of polyethylene generated in the latter half of the polymerization process or in the post-polymerization process.
  • kneading energy (E 0 ) at the start of swelling is preferably 5% or less, more preferably 1% or less, and even more preferably 0.1% or less, of the total kneading energy (E t ).
  • the lower limit is not particularly limited, and is generally 0% or more.
  • the kneading energy (E 0 ) at the start of swelling in the present embodiment is an integrated value of torque per unit volume from the start of kneading of the polyethylene powder to the start of temperature rise. This value takes a value greater than 0 when there is a polyethylene component with a low melting point, which begins to melt before swelling, on the powder surface.
  • the kneading energy (E 0 ) at the start of swelling is 5% or less of the total kneading energy (E t ), the generation of unmelted materials is suppressed, and it tends to be possible to produce a microporous membrane with a more excellent appearance.
  • the amount of comonomers is adjusted in the first half of the polymerization process.
  • the kneading energy (E 0 ) at the start of swelling of the present embodiment can be specifically measured by the method described in the Examples, described later.
  • the range of the median diameter is preferably 50 ⁇ m or more and 250 ⁇ m or less, more preferably 60 ⁇ m or more and 200 ⁇ m or less, and even more preferably 70 ⁇ m or more and 150 ⁇ m or less.
  • the median diameter of the polyethylene powder of the present embodiment is the particle diameter (D50) at which the cumulative mass is 50%.
  • the median diameter is 50 ⁇ m or more, the ease of handling the polyethylene powder (improvement of fluidity, suppression of dust, etc.) in the production process and extrusion process is improved.
  • the plasticizer is likely to impregnate the center of the polyethylene powder, and the generation of unmelted materials is suppressed.
  • the particle diameter of the polymerization catalyst is controlled, or the polymerization conditions, described later, are adjusted so as to prevent the rapid progress of the polymerization reaction (hereinafter also referred to as rapid polymerization).
  • the median diameter of the polyethylene powder of the present embodiment can be specifically measured by the method described in the Examples, described later.
  • the density range of the polyethylene powder of the present embodiment is preferably 920 kg/m 3 or more and 960 kg/m 3 or less, more preferably 930 kg/m 3 or more and 955 kg/m 3 or less, and even more preferably 935 kg/m 3 or more and 950 kg/m 3 or less.
  • the microporous membrane using the polyethylene powder of the present embodiment has excellent balance between dimensional stability and mechanical strength.
  • the density of the polyethylene powder of the present embodiment can be controlled within the above numerical range, for example, by adjusting the amount of comonomers other than ethylene in the polymerization process, or by adjusting the molecular weight of the polymer.
  • the density of the polyethylene powder of the present embodiment can be specifically measured by the method described in the Examples, described later.
  • the polyethylene powder of the present embodiment can be produced by polymerizing ethylene, or ethylene and other comonomers, using a predetermined catalyst component.
  • the catalyst component used in the production of the ethylene-based polymer that constitutes the polyethylene powder of the present embodiment is not particularly limited, and examples include a Ziegler-Natta catalyst and a metallocene catalyst.
  • Examples of the method for producing a Ziegler-Natta catalyst or a metallocene catalyst include the methods disclosed in Japanese Patent No. 5782558 and Japanese Patent Laid-Open No. 2019-19265 .
  • Examples of the polymerization method of the ethylene-based polymer that constitutes the polyethylene powder of the present embodiment include a method of polymerizing ethylene or a method of copolymerizing ethylene and a comonomer, by suspension polymerization or gas-phase polymerization.
  • suspension polymerization which can efficiently remove the heat of polymerization.
  • an inert hydrocarbon solvent can be used as a solvent.
  • an olefin itself can be used as a solvent.
  • the inert hydrocarbon solvent is not particularly limited, and examples include aliphatic hydrocarbons, such as propane, butane, isobutane, pentane, isopentane, hexane, heptane, octane, decane, dodecane, and kerosene; alicyclic hydrocarbons, such as cyclopentane, cyclohexane, and methylcyclopentane; aromatic hydrocarbons, such as benzene, toluene, and xylene; halogenated hydrocarbons, such as ethyl chloride, chlorobenzene, and dichloromethane; and mixtures thereof.
  • aliphatic hydrocarbons such as propane, butane, isobutane, pentane, isopentane, hexane, heptane, octane, decane, dodecane, and kerosene
  • alicyclic hydrocarbons
  • the polymerization temperature in the polymerization process of the ethylene-based polymer is preferably 40°C or more and 100°C or less, more preferably 45°C or more and 95°C or less, and even more preferably 50°C or more and 90°C or less.
  • a polymerization temperature of 40°C or more enables industrially efficient production.
  • a polymerization temperature of 100°C or less makes it possible to suppress the generation of massive scales when a part of the polymer melts, thus enabling continuous and stable production of the ethylene-based polymer without pipe clogging.
  • the polymerization pressure in the polymerization process of the ethylene-based polymer is preferably ordinary pressure or more and 2 MPaG or less, more preferably 0.2 MPaG or more and 1.5 MPaG or less, and even more preferably 0.3 MPaG or more and 0.9 MPaG or less.
  • a polymerization pressure equal to or higher than ordinary pressure enables industrially efficient production.
  • a polymerization pressure of 2 MPaG or less makes it possible to prevent the generation of massive scales due to rapid polymerization in the polymerization reactor, and tends to enable stable production.
  • an antistatic agent such as Stadis or STATSAFE produced by Innospec (distributor: Maruwa Bussan K.K.), in order to suppress electrostatic adhesion of the ethylene-based polymer to the polymerization reactor.
  • the antistatic agent such as Stadis or STATSAFE, may be added to a solid catalyst in advance, but may be diluted with an inert hydrocarbon solvent and then added to the polymerization reactor by a pump or the like.
  • the amount of antistatic agent added is preferably 1 ppm or more and 500 ppm or less, and more preferably 10 ppm or more and 100 ppm or less, based on the production volume of the ethylene-based polymer per unit time.
  • the molecular weight of the ethylene-based polymer can be adjusted, for example, by allowing hydrogen to be present in the polymerization system, or changing the polymerization temperature, as described in West German Patent Application No. 3127133 .
  • the molecular weight of the ethylene-based polymer can be controlled within an appropriate range by adding hydrogen as a chain transfer agent into the polymerization system.
  • the range of the mole fraction of hydrogen is preferably 0 mol% or more and 50 mol% or less, and more preferably 0 mol% or more 30 mol% or less.
  • the polymerization reaction can be performed in a batch, semi-continuous, or continuous manner, and preferably in a continuous manner.
  • the polymerization reaction of the ethylene-based polymer may be performed by a single-stage polymerization method using one polymerization reactor, or a multistage polymerization method in which polymerization is performed continuously in sequence in two or more polymerization reactors connected in series. In terms of capable of efficiently controlling the structure of the surface and center of the polyethylene powder, it is preferable to use a multistage polymerization method.
  • the production of an ethylene-based polymer using a multistage polymerization method is specifically performed in the following manner.
  • an ethylene-based polymer X is produced in a first-stage polymerization reactor using the above production conditions, and the ethylene-based polymer X extracted from the first-stage polymerization reactor is transferred to an intermediate flash tank to separate unreacted ethylene and hydrogen, and comonomers when copolymerization is performed in the first-stage polymerization reactor.
  • the suspension containing the ethylene-based polymer X is transferred to a second-stage polymerization reactor, and an ethylene-based polymer Y is produced using the above production conditions.
  • the difference between the temperature of the first-stage polymerization reactor and the temperature of the second-stage polymerization reactor preferably satisfies the following ⁇ Formula 1>, more preferably satisfies the following ⁇ Formula 2>, and even more preferably satisfies the following ⁇ Formula 3>.
  • the mobility of the molecular chains on the surface of the polyethylene powder is improved, and the pressure from the molecular chains growing inside the polyethylene powder is increased. From these, by satisfying the above ⁇ Formula 1> to ⁇ Formula 3>, the amount of entanglement of molecular chains on the surface of the polyethylene powder is small, and the molecular chains are easily dispersed in the kneading process. In addition, the pores are sufficiently expanded, and the impregnability of the plasticizer can be further enhanced.
  • the pressure of the intermediate flash tank described above is preferably 0.01 MPaG or more and 0.2 MPaG or less.
  • the temperature of the intermediate flash tank is preferably 70°C or more and 100°C or less. Further, it is preferable to feed comonomers into the flash tank.
  • the ratio of the ethylene-based polymer Y contained in the polyethylene powder produced by the multistage polymerization method described above, that is, the range of the production volume of the ethylene polymer in the second-stage polymerization reactor, i.e., the content, is preferably 30% to 70%, more preferably 35% to 65%, and even more preferably 40% to 65%.
  • the pores on the surface of the polyethylene powder can be expanded to further enhance the impregnability of the plasticizer.
  • the density range is preferably 930 kg/m 3 or more and 960 kg/m 3 or less, more preferably 935 kg/m 3 or more and 960 kg/m 3 or less, and even more preferably 940 kg/m 3 or more and 960 kg/m 3 or less.
  • the range of the viscosity average molecular weight of the ethylene-based polymer X is not particularly limited, as long as the viscosity average molecular weight of the finally generated polyethylene powder is within the above range.
  • the density range is preferably 920 kg/m 3 or more and 950 kg/m 3 or less, and more preferably 920 kg/m 3 or more and 945 kg/m 3 or less.
  • the range of the viscosity average molecular weight of the ethylene-based polymer Y is not particularly limited, as long as the viscosity average molecular weight of the finally generated polyethylene powder is within the above range; however, in terms of reducing the amount of plasticizer required during molding, this range is preferably 10,000 or more and 2,000,000 or less, and more preferably 10,000 or more and 1,500,000 or less.
  • the viscosity average molecular weight and density can be determined in such a manner that after the physical property values of the ethylene-based polymer X extracted from the first-stage polymerization reactor and the finally produced polyethylene powder are measured, the viscosity average molecular weight and density can be determined based on additivity from the production volume of each polymerization reactor.
  • the suspension containing the ethylene-based polymer that constitutes the polyethylene powder of the present embodiment is quantitatively extracted from the polymerization reactor and transferred to a final flash tank to separate unreacted ethylene and hydrogen, and other comonomers when copolymerization is performed in the polymerization reactor.
  • the pressure of the final flash tank is preferably 0.05 MPaG or more and 0.5 MPaG or less, and the temperature is preferably 70°C or more and 100°C or less. Further, it is preferable to feed other comonomers.
  • the solvent is separated after the polymerization process.
  • the solvent separation method any of decantation, centrifugal separation, filter filtration, and the like can be applied; however, centrifugal separation is more preferred because it can separate the ethylene-based polymer and the solvent efficiently.
  • the solvent content of the ethylene-based polymer after solvent separation is not particularly limited, but is preferably 20 mass% or more and 70 mass% or less, and more preferably 30 mass% or more and 60 mass% or less, based on the mass of the ethylene-based polymer.
  • the solvent content is 20 mass% or more, post-polymerization tends to progress at the center of the polyethylene powder, and the surface of the polyethylene powder tends to be stretched.
  • the low-molecular-weight component, i.e., wax, contained in the solvent is less likely to remain in the polyethylene powder, and it is possible to suppress reduction in heat resistance of the microporous membrane due to inclusion of wax.
  • the catalyst used in the polymerization process is deactivated after the polymerization process.
  • the deactivation of the catalyst is preferably performed after separating the ethylene-based polymer and the solvent.
  • catalyst-deactivating agents include oxygen, water, alcohols, glycols, phenols, carbon monoxide, carbon dioxide, ethers, carbonyl compounds, and alkynes.
  • a drying process is performed after the solvent is separated.
  • the drying temperature is preferably 50°C or more and 150°C or less, and more preferably 70°C or more and 110°C or less.
  • the resultant may be sieved to remove coarse particles.
  • the polyethylene powder of the present embodiment may be a mixture of multiple polyethylene powders including an ethylene-based polymer obtained by the above production method.
  • the polyethylene powder of the present embodiment may be used in combination with known additives, such as slip agents, neutralizers, antioxidants, light-resistant stabilizers, antistatic agents, and pigments.
  • additives such as slip agents, neutralizers, antioxidants, light-resistant stabilizers, antistatic agents, and pigments.
  • slip agents or neutralizers include, but are not particularly limited to, aliphatic hydrocarbons, higher fatty acids, higher fatty acid metal salts, fatty acid esters of alcohols, waxes, higher fatty acid amides, silicone oil, and rosin. Specifically, calcium stearate, magnesium stearate, zinc stearate, and other stearates can be used as preferable additives.
  • antioxidants include, but are not particularly limited to, phenol-based compounds, phenol phosphate-based compounds, and phosphorus-based compounds.
  • Specific examples include phenol-based antioxidants, such as 2,6-di-t-butyl-4-methylphenol(dibutylhydroxytoluene), n-octadecyl-3-(4-hydroxy-3,5-di-t-butylphenyl)propionate, and tetrakis(methylene(3,5-di-t-butyl-4-hysaloxyhydrocinnamate))methane; phenol phosphate-based antioxidants, such as 6-[3-(3-t-butyl-4-hydroxy-5-methylphenyl)propoxy]-2,4,8,10-tetra-t-butyldibenzo[d,f][1,3,2]dioxaphosphepin; and phosphate-based antioxidants, such as tetrakis(2,4-d
  • light-resistant stabilizers include, but are not particularly limited to, benzotriazole-based light-resistant stabilizers, such as 2-(5-methyl-2-hydroxyphenyl)benzotriazole and 2-(3-t-butyl-5-methyl-2-hydroxyphenyl)-5-chlorobenzotriazole; and hindered amine-based light-resistant stabilizers, such as bis(2,2,6,6-tetramethyl-4-piperidine)sebacate and poly[ ⁇ 6-(1,1,3,3-tetramethylbutyl)amino-1,3,5-triazine-2,4-diyl ⁇ (2,2,6,6-tetramethyl-4-piperidyl)imino ⁇ hexamethylene ⁇ (2,2,6,6-tetramethyl-4-piperidyl)imino ⁇ ].
  • benzotriazole-based light-resistant stabilizers such as 2-(5-methyl-2-hydroxyphenyl)benzotriazole and 2-(3-t-butyl-5-methyl-2
  • antistatic agents include, but are not particularly limited to, aluminosilicate, kaolin, clay, natural silica, synthetic silica, silicates, talc, diatomaceous earth, and glycerol fatty acid esters.
  • the polyethylene powder of the present embodiment can be used as a raw material for various molded articles, such as microporous membranes, high-strength fibers, sintered compacts, press-molded articles, and ram press-molded articles.
  • the polyethylene powder of the present embodiment is suitable as a raw material for microporous membranes for battery separators.
  • the molded article of the present embodiment is a molded article of the polyethylene powder of the present embodiment described above.
  • the molded article of the present embodiment is obtained, for example, by introducing the polyethylene powder of the present embodiment into an extruder, and molding it into a desired shape, such as a sheet shape, followed by a drying process.
  • Examples of the molded article of the present embodiment include microporous membranes, specifically battery separators, and more specifically lithium ion secondary battery separators, lead-acid battery separators, and the like.
  • Examples of the method for producing the microporous membrane include a molding method comprising the steps of extruding, drawing, extracting, and drying resin using a wet extrusion method.
  • the viscosity average molecular weight of the polyethylene powder was measured according to ISO1628-3 (2010) in the following manner.
  • the polyethylene powder was weighed in the range of 4.0 to 4.5 mg into a dissolution tube.
  • the weighed mass is expressed as "m (unit: mg)" in the following mathematical formula.
  • 20 mL of decahydronaphthalene containing 1 g/L of 2,6-di-t-butyl-4-methylphenol; hereinafter referred to as decalin
  • decalin decahydronaphthalene
  • Viscosity average molecular weight Mv 5.34 ⁇ 10 4 ⁇ ⁇ 1.49
  • the slope of a straight line connecting two local maximum points in a torque curve obtained when kneading the polyethylene powder was determined in the following manner.
  • liquid paraffin product name: P-350P
  • unit model: 30C150, mixer model: R-60 Labo Plastomill Mixer
  • a torque curve was obtained by plotting the average torque (rotational load generated during kneading) calculated by Labo Plastomill Mixer Test Program Ver. 4.52 (Copyright (C) Toyo Seiki Seisaku-sho, Ltd.) on the vertical axis, and the kneading time on the horizontal axis. At this time, the average torque value was plotted every 0.125 seconds.
  • the ratio of kneading energy (E A ) during swelling to kneading energy (E B ) during melting in the torque curve was determined in the following manner.
  • Kneading energy (E 0 ) at the start of swelling was determined in the following manner.
  • the median diameter of the polyethylene powder was determined in the following manner.
  • the polyethylene powder was classified with a sieve according to JIS Z8801 standard.
  • the sieve mesh sizes used were 425 ⁇ m, 300 ⁇ m, 212 ⁇ m, 150 ⁇ m, 106 ⁇ m, 75 ⁇ m, and 53 ⁇ m, and the mass of the polyethylene powder collected for each fraction was measured. Then, the fraction (mass%) of each fraction to the total mass of the polyethylene powder before classification was calculated, and the cumulative undersize percentage (mass%), which is the percentage integrated from the smaller mesh size, was determined.
  • the density of the polyethylene powder was determined by the methods (1) to (7) shown below.
  • the obtained powder mixture was injected into a twin-screw extruder through a feeder under a nitrogen atmosphere.
  • liquid paraffin P-350P (trademark), produced by MORESCO Corporation
  • P-350P liquid paraffin
  • the mixture was kneaded at 160°C, extruded through a T-die installed at the tip of the extruder, and then immediately cooled and solidified on a cast roll cooled to 25°C to form a gel-like sheet with a thickness of 1200 ⁇ m.
  • This gel-like sheet was stretched 7 ⁇ 7 times at 115 to 125°C using a simultaneous biaxial stretching machine, and the stretched film was immersed in methyl ethyl ketone for 30 minutes to remove the liquid paraffin by extraction, followed by drying.
  • the film was further heat-set at 115°C to 125°C for 3 minutes to obtain a microporous membrane.
  • the stretching temperature and heat-setting temperature were appropriately adjusted for each microporous membrane within the specified temperatures.
  • the number of defects present in the microporous membrane of 250 mm ⁇ 250 mm obtained by the (Method for Producing Microporous Membrane) described above was visually counted.
  • impurities such as dust observed as black spots were excluded.
  • the number of defects was evaluated according to the following evaluation criteria.
  • the measurement was performed at 3 points per microporous membrane of 100 mm ⁇ 50 mm.
  • the standard deviation of 24 measurements in total was calculated, and the uniformity of air permeability was evaluated according to the following evaluation criteria. This was used for the evaluation of the uniformity of the pore structure of the microporous membrane.
  • microporous membrane obtained by the (Method for Producing Microporous Membrane) described above was impregnated with an electrolytic solution, a cell was produced by sandwiching this membrane between SUS plate electrodes, and the AC resistance of the cell was measured while the temperature was raised.
  • the temperature at which the resistance suddenly increased was taken as the shutdown temperature, and evaluated according to the following evaluation criteria.
  • a Ziegler-Natta Catalyst (A) was prepared according to the following (1) to (4).
  • the reaction was continued at 10°C for 1 hour. After completion of the reaction, the supernatant was removed, followed by washing four times with hexane to remove unreacted raw material components, thereby preparing a Ziegler-Natta catalyst (B).
  • an ethylene-based polymer (X A ) was polymerized in the first-stage reactor, and an ethylene-based polymer (Y A ) was polymerized in the second-stage reactor, thereby obtaining a polyethylene powder (A).
  • the polyethylene powder (A) had a viscosity average molecular weight of 270,000, a density of 945 kg/m 3 , and a median diameter of 89 ⁇ m.
  • the ethylene-based polymer was polymerized using a vessel type 300L polymerization reactor equipped with three swept-back stirring blades and three baffles.
  • normal hexane As a solvent, normal hexane was supplied at a flow rate of 40 L/h, and the stirring speed was set to 230 rpm.
  • the Ziegler-Natta catalyst (A) As a polymerization catalyst, the Ziegler-Natta catalyst (A) was used and supplied so that the production speed of the ethylene-based polymer was 7.1 kg/h.
  • a cocatalyst component a mixture of triisobutylaluminum and diisobutylaluminum hydride (9:1) was used and supplied at 10 mmol/h. 23 mol% (molar ratio: hydrogen/(ethylene+hydrogen)) of hydrogen was supplied.
  • the polymerization temperature was set to 50°C
  • the polymerization pressure was set to 0.37 MPaG
  • the average residence time was set to 3.3 hours.
  • the ethylene-based polymer (X A ) obtained as described above had a viscosity average molecular weight of 680,000 and a density of 943 kg/m 3 . Further, the polymerization activity in the first-stage reactor was 20,600 g per gram of the catalyst.
  • the polymerization slurry in the polymerization reactor was guided to an intermediate flash tank with a pressure of 0.13 MPaG and a temperature of 80°C so that the level in the polymerization reactor was kept constant, and unreacted ethylene and hydrogen were separated. 15 mol% (molar ratio: (1-butene)/(ethylene+hydrogen+(1-butene))) of 1-butene was supplied to the intermediate flash tank, and the average residence time was set to 1.3 hours.
  • the polymerization slurry containing the ethylene-based polymer (X A ) was transferred from the intermediate flash tank to a vessel type 300L polymerization reactor equipped with three swept-back stirring blades and three baffles, followed by polymerization of the ethylene-based polymer (Y A ).
  • the stirring speed was set to 196 rpm, and as a cocatalyst component, a mixture of triisobutylaluminum and diisobutylaluminum hydride (9:1) was supplied at 10 mmol/h. 26 mol% (molar ratio: hydrogen/(ethylene+hydrogen+(1-butene))) of hydrogen was supplied, and 5.2 mol% (molar ratio: (1-butene)/(ethylene+hydrogen+(1-butene))) of 1-butene was supplied as a comonomer.
  • the polymerization temperature was set to 83°C
  • the polymerization pressure was set to 0.58 MPaG so that the production speed was 12.7 kg/h
  • the average residence time was set to 0.75 hours.
  • the thus-obtained ethylene-based polymer (Y A ) had a viscosity average molecular weight of 40,000 and a density of 946 kg/m 3 .
  • the polymerization activity in the second-stage reactor was 8,300 g per gram of the catalyst.
  • the polymerization slurry in the polymerization reactor was guided to a final flash tank with a pressure of 0.05 MPaG and a temperature of 80°C so that the level in the polymerization reactor was kept constant, and unreacted ethylene and hydrogen were separated.
  • the average residence time in the final flash tank was set to 1 hour.
  • the polymerization slurry was continuously transferred by a pump from the flash tank to a centrifuge, and the polymer and the solvent were separated. Then, the separated ethylene-based polymer was transferred to a rotary kiln dryer controlled to 85°C, and dried while blowing nitrogen, thereby obtaining a polyethylene powder (A).
  • the polyethylene powder was sprayed with steam to deactivate the catalyst and cocatalyst.
  • an ethylene-based polymer (X B ) was polymerized in the first-stage reactor, and an ethylene-based polymer (Y B ) was polymerized in the second-stage reactor, thereby obtaining a polyethylene powder (B).
  • the polyethylene powder (B) had a viscosity average molecular weight of 290,000, a density of 942 kg/m 3 and a median diameter of 96 ⁇ m.
  • Polymerization was carried out in the same manner as in the polymerization of (X A ) in Example 1, except that the production speed was changed to 7.2 kg/h, the amount of hydrogen supplied was changed to 16 mol%, the polymerization temperature was changed to 57°C, and the polymerization pressure was changed to 0.3 MPaG, thereby obtaining an ethylene-based polymer (X B ).
  • the obtained ethylene-based polymer (X B ) had a viscosity average molecular weight of 690,000 and a density of 942 kg/m 3 . Further, the polymerization activity in the first-stage reactor was 30,000 g per gram of the catalyst.
  • the polymerization slurry in the polymerization reactor was guided to an intermediate flash tank that was set under the same conditions as for (X A ) of Example 1, except that the pressure was changed to 0.1 MPaG.
  • Polymerization was carried out in the same manner as in the polymerization of (Y A ) in Example 1, except that the production speed was changed to 11.8 kg/h, the amount of hydrogen supplied was changed to 22 mol%, the polymerization temperature was changed to 85°C, the polymerization pressure was changed to 0.56 MPaG, and the amount of 1-butene supplied was changed to 7.4 mol%, thereby obtaining an ethylene-based polymer (Y B ).
  • the obtained ethylene-based polymer (Y B ) had a viscosity average molecular weight of 45,000 and a density of 942 kg/m 3 . Further, the polymerization activity in the second-stage reactor was 11,000 g per gram of the catalyst.
  • the polymerization slurry in the polymerization reactor was guided to a final flash tank that was set under the same conditions as for (Y A ) of Example 1, except that 15 mol% of 1-butene was supplied. Then, the polymerization slurry was separated and dried in the same manner as for (Y A ) of Example 1, thereby obtaining a polyethylene powder (B).
  • an ethylene-based polymer (X C ) was polymerized in the first-stage reactor, and an ethylene-based polymer (Y C ) was polymerized in the second-stage reactor, thereby obtaining a polyethylene powder (C).
  • the polyethylene powder (C) had a viscosity average molecular weight of 240,000, a density of 944 kg/m 3 , and a median diameter of 102 ⁇ m.
  • Polymerization was carried out in the same manner as in the polymerization of (X A ) in Example 1, except that the production speed was changed to 12.8 kg/h, the amount of hydrogen supplied was changed to 44 mol%, the polymerization temperature was changed to 78°C, the polymerization pressure was changed to 0.65 MPaG, the average residence time was changed to 3 hours, and 5.7 mol% of 1-butene was supplied as a comonomer, thereby obtaining an ethylene-based polymer (X C ).
  • the obtained ethylene-based polymer (X C ) had a viscosity average molecular weight of 60,000 and a density of 947 kg/m 3 . Further, the polymerization activity in the first-stage reactor was 57,000 g per gram of the catalyst.
  • the polymerization slurry in the polymerization reactor was guided to an intermediate flash tank that was set under the same conditions as for (X A ) of Example 1, except that the pressure was changed to 0.2 MPaG.
  • Polymerization was carried out in the same manner as in the polymerization of (Y A ) in Example 1, except that the production speed was changed to 7.2 kg/h, the amount of hydrogen supplied was changed to 3 mol%, the polymerization temperature was changed to 78°C, the polymerization pressure was changed to 0.29 MPaG, the amount of 1-butene supplied was changed to 1.1 mol%, and the average residence time was changed to 0.82 hours, thereby obtaining an ethylene-based polymer (Y C ).
  • the obtained ethylene-based polymer (Y C ) had a viscosity average molecular weight of 560,000 and a density of 939 kg/m 3 . Further, the polymerization activity in the second-stage reactor was 8,500 g per gram of the catalyst.
  • the polymerization slurry in the polymerization reactor was guided to a final flash tank that was set under the same conditions as for (Y B ) of Example 2. Then, the polymerization slurry was separated and dried in the same manner as for (Y A ) of Example 1, thereby obtaining a polyethylene powder (C).
  • the polyethylene powder was polymerized using a vessel type 300L polymerization reactor equipped with three swept-back stirring blades and three baffles.
  • a solvent normal hexane was supplied at a flow rate of 80 L/h, and the stirring speed was set to 230 rpm.
  • the Ziegler-Natta catalyst (A) was used and supplied so that the production speed of the polyethylene powder was 9 kg/h.
  • the antistatic agent STATSAFE 3000 (90 g/L) produced by Innospec diluted with normal hexane was added to the polymerization catalyst in an amount of 20 mass ppm with respect to the production speed of the polyethylene powder.
  • a cocatalyst component a mixture of triisobutylaluminum and diisobutylaluminum hydride (9:1) was used and supplied at 10 mmol/h. 2.7 mol% (molar ratio: hydrogen/(ethylene+hydrogen)) of hydrogen was supplied.
  • the polymerization temperature was set to 78°C
  • the polymerization pressure was set to 0.3 MPaG
  • the average residence time was set to 1.7 hours.
  • the polymerization slurry in the polymerization reactor was guided to a final flash tank with a pressure of 0.3 MPaG and a temperature of 80°C so that the level in the polymerization reactor was kept constant, and unreacted ethylene and hydrogen were separated. 15 mol% (molar ratio: (1-butene)/(ethylene+hydrogen+(1-butene))) of 1-butene was supplied to the final flash tank, and the average residence time in the final flash tank was set to 1 hour.
  • the polymerization slurry was continuously transferred by a pump from the flash tank to a centrifuge, and the polymer and the solvent were separated. Then, the separated polyethylene powder was transferred to a rotary kiln dryer controlled to 85°C and dried while blowing nitrogen.
  • the polyethylene powder was sprayed with steam to deactivate the catalyst and cocatalyst.
  • the polyethylene powder (D) obtained as described above had a viscosity average molecular weight of 700,000, a density of 936 kg/m 3 , and a median diameter of 108 ⁇ m. Further, the polymerization activity in the reactor was 11,500 g per gram of the catalyst.
  • the above various evaluations were performed on the polyethylene powder (D), and a microporous membrane of the polyethylene powder (D) produced by the (Method for Producing Microporous Membrane) described above, and the results are shown in Table 1.
  • polyethylene powder (D) 50 parts by mass of the polyethylene powder (D) was added to 50 parts by mass of a polyethylene powder (E) polymerized as shown below, and the mixture was dry-blended using a tumbler blender, thereby obtaining a polyethylene powder (F).
  • the polyethylene powder (F) had a viscosity average molecular weight of 500,000, a density of 941 kg/m 3 and a median diameter of 99 ⁇ m.
  • polymerization was carried out under the same conditions as in Example 4, except that the amount of hydrogen added was changed to 6 mol%.
  • the obtained polyethylene powder (E) had a viscosity average molecular weight of 300,000, a density of 945 kg/m 3 , and a median diameter of 90 ⁇ m. Further, the polymerization activity in the reactor was 11,600 g per gram of the catalyst.
  • an ethylene-based polymer (X G ) was polymerized in the first-stage reactor, and an ethylene-based polymer (Y G ) was polymerized in the second-stage reactor, thereby obtaining a polyethylene powder (G).
  • the polyethylene powder (G) had a viscosity average molecular weight of 900,000, a density of 941 kg/m 3 and a median diameter of 90 ⁇ m.
  • Polymerization was carried out in the same manner as in the polymerization of (X A ) in Example 1, except that the polymerization catalyst was changed to the Ziegler-Natta catalyst (B), the production speed was changed to 6.9 kg/h, the amount of hydrogen supplied was changed to 0.95 mol%, and the polymerization pressure was changed to 0.3 MPaG, thereby obtaining an ethylene-based polymer (X G ).
  • the obtained ethylene-based polymer (X G ) had a viscosity average molecular weight of 2,000,000 and a density of 937 kg/m 3 . Further, the polymerization activity in the first-stage reactor was 19,500 g per gram of the catalyst.
  • the polymerization slurry in the polymerization reactor was guided to an intermediate flash tank that was set under the same conditions as for (X A ) of Example 1, except that the pressure was changed to 0.1 MPaG, and 1-butene was not supplied.
  • Polymerization was carried out in the same manner as in the polymerization of (Y A ) in Example 1, except that the production speed was changed to 12.9 kg/h, the amount of hydrogen supplied was changed to 14.4 mol%, the polymerization temperature was changed to 85°C, and the amount of 1-butene supplied was changed to 10.5 mol%, thereby obtaining an ethylene-based polymer (Y G ).
  • the obtained ethylene-based polymer (Y G ) had a viscosity average molecular weight of 300,000 and a density of 944 kg/m 3 . Further, the polymerization activity in the second-stage reactor was 33,000 g per gram of the catalyst.
  • the polymerization slurry in the polymerization reactor was guided to a final flash tank that was set under the same conditions as for (Y A ) of Example 1. Then, the polymerization slurry was separated and dried in the same manner as for (Y A ) of Example 1, thereby obtaining a polyethylene powder (G).
  • Polymerization was carried out under the same conditions as in Example 4, except that the polymerization catalyst was changed to the Ziegler-Natta catalyst (B), the production speed was changed to 10.0 kg/h, and the amount of hydrogen added was changed to 0.56 mol%.
  • the polymerization catalyst was changed to the Ziegler-Natta catalyst (B)
  • the production speed was changed to 10.0 kg/h
  • the amount of hydrogen added was changed to 0.56 mol%.
  • the obtained polyethylene powder (H) had a viscosity average molecular weight of 1,500,000, a density of 930 kg/m 3 , and a median diameter of 82 ⁇ m.
  • the polymerization activity in the reactor was 59,500 g per gram of the catalyst.
  • the polyethylene powder (K) had a viscosity average molecular weight of 280,000, a density of 946 kg/m 3 , and a median diameter of 76 ⁇ m.
  • Polymerization was carried out under the same conditions as in Example 4, except that the flow rate of normal hexane was changed to 40 L/h, the production speed was changed to 7.1 kg/h, the amount of hydrogen added was changed to 23 mol%, the polymerization temperature was changed to 50°C, the polymerization pressure was changed to 0.37 MPaG, the average residence time was changed to 3.3 hours, the pressure of the final flash tank was changed to 0.05 MPaG, and 1-butene was not supplied to the final flash tank.
  • the obtained polyethylene powder (I) had a viscosity average molecular weight of 680,000, a density of 943 kg/m 3 , and a median diameter of 79 ⁇ m. Further, the polymerization activity in the reactor was 20,600 g per gram of the catalyst.
  • Polymerization was carried out under the same conditions as in Example 4, except that the flow rate of normal hexane was changed to 40 L/h, the production speed was changed to 12.8 kg/h, the amount of hydrogen added was changed to 44 mol%, the polymerization pressure was changed to 0.65 MPaG, the average residence time was changed to 3 hours, 5.7 mol% of 1-butene was supplied, the pressure of the final flash tank was changed to 0.05 MPaG, and 1-butene was not supplied to the final flash tank.
  • the obtained polyethylene powder (J) had a viscosity average molecular weight of 60,000, a density of 947 kg/m 3 , and a median diameter of 75 ⁇ m.
  • the polymerization activity in the reactor was 57,200 g per gram of the catalyst.
  • an ethylene-based polymer (X L ) was polymerized in the first-stage reactor, and an ethylene-based polymer (Y L ) was polymerized in the second-stage reactor, thereby obtaining a polyethylene powder (L).
  • the polyethylene powder (L) had a viscosity average molecular weight of 280,000, a density of 942 kg/m 3 , and a median diameter of 115 ⁇ m.
  • Polymerization was carried out in the same manner as in the polymerization of (X A ) in Example 1, except that the flow rate of normal hexane was changed to 80 L/h, the amount of hydrogen supplied was changed to 2.8 mol%, the polymerization temperature was changed to 78°C, the polymerization pressure was changed to 0.3 MPaG, the average residence time was changed to 1.7 hours, and 4.8 mol% of 1-butene was supplied, thereby obtaining an ethylene-based polymer (X L ).
  • the obtained ethylene-based polymer (X L ) had a viscosity average molecular weight of 710,000 and a density of 942 kg/m 3 . Further, the polymerization activity in the first-stage reactor was 20,900 g per gram of the catalyst.
  • the polymerization slurry in the polymerization reactor was guided to an intermediate flash tank that was set under the same conditions as for (X A ) of Example 1, except that the pressure was changed to 0.1 MPaG.
  • Polymerization was carried out in the same manner as in the polymerization of (Y A ) in Example 1, except that the amount of hydrogen supplied was changed to 29 mol%, the polymerization temperature was changed to 78°C, and the polymerization pressure was changed to 0.65 MPaG, thereby obtaining an ethylene-based polymer (Y L ).
  • the obtained ethylene-based polymer (Y L ) had a viscosity average molecular weight of 45,000 and a density of 942 kg/m 3 . Further, the polymerization activity in the second-stage reactor was 12,000 g per gram of the catalyst.
  • the polymerization slurry in the polymerization reactor was guided to a final flash tank that was set under the same conditions as for (Y A ) of Example 1. Then, the polymerization slurry was separated and dried in the same manner as for (Y A ) of Example 1, thereby obtaining a polyethylene powder (L).
  • Polymerization was carried out under the same conditions as in Example 4, except that the polymerization catalyst was changed to the Ziegler-Natta catalyst (B), the flow rate of normal hexane was changed to 40 L/h, the production speed was changed to 13.1 kg/h, the amount of hydrogen added was changed to 13 mol%, the polymerization temperature was changed to 83°C, the polymerization pressure was changed to 0.37 MPaG, the average residence time was changed to 3 hours, the pressure of the final flash tank was changed to 0.05 MPaG, and 1-butene was not supplied to the final flash tank.
  • B Ziegler-Natta catalyst
  • the obtained polyethylene powder (M) had a viscosity average molecular weight of 310,000, a density of 953 kg/m 3 , and a median diameter of 94 ⁇ m.
  • the polymerization activity in the reactor was 41,900 g per gram of the catalyst.
  • the above various evaluations were performed on the polyethylene powder (M), and a microporous membrane of the polyethylene powder (M) produced by the (Method for Producing Microporous Membrane) described above, and the results are shown in Table 1.
  • the polyethylene powder of the present invention is industrially applicable as a raw material for various molded articles, microporous membranes, and battery separators.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Medicinal Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Electrochemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Manufacture Of Porous Articles, And Recovery And Treatment Of Waste Products (AREA)
  • Compositions Of Macromolecular Compounds (AREA)
  • Processes Of Treating Macromolecular Substances (AREA)
EP21894564.0A 2020-11-17 2021-11-12 Poudre de polyéthylène et corps moulé Pending EP4249523A4 (fr)

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JPS5840743U (ja) 1981-09-11 1983-03-17 コピア株式会社 焼付ガラスのクリ−ニング装置
JPS6135665U (ja) 1984-07-31 1986-03-05 ダイキン工業株式会社 食器洗浄機
JPH07238109A (ja) * 1994-03-01 1995-09-12 Ube Ind Ltd エチレンの重合及び共重合方法
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EP2414087B1 (fr) 2009-03-30 2019-01-16 Toray Industries, Inc. Membranes microporeuses, procédé de fabrication et utilisation de ces membranes en tant que film séparateur de batteries
WO2013141306A1 (fr) 2012-03-23 2013-09-26 東レ株式会社 Film poreux et dispositif de stockage électrique
JP6281372B2 (ja) 2013-03-29 2018-02-21 日本ポリエチレン株式会社 ポリエチレン系樹脂組成物及びそれよりなる成形体
JP5840743B2 (ja) 2013-09-05 2016-01-06 旭化成ケミカルズ株式会社 ポリエチレン樹脂組成物、微多孔性フィルム及びその製造方法、並びに、電池用セパレーター
JP6294639B2 (ja) * 2013-11-26 2018-03-14 旭化成株式会社 ポリエチレン樹脂組成物及び高純度薬品用容器
JP5782558B1 (ja) 2014-11-14 2015-09-24 旭化成ケミカルズ株式会社 ポリエチレンパウダー
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JP7001382B2 (ja) 2017-07-20 2022-02-03 旭化成株式会社 ポリエチレンパウダー
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WO2020179650A1 (fr) * 2019-03-01 2020-09-10 旭化成株式会社 Poudre de polyéthylène, et corps moulé constitué par moulage de celle-ci
WO2020189443A1 (fr) * 2019-03-18 2020-09-24 旭化成株式会社 Poudre de polyéthylène et corps moulé de celle-ci
JP2020191016A (ja) 2019-05-23 2020-11-26 富士通株式会社 情報処理プログラム、情報処理装置及び情報処理方法
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JPWO2022107690A1 (fr) 2022-05-27
WO2022107690A1 (fr) 2022-05-27

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